EP0093051B1 - Resorptionsverfahren für Wärmepumpen - Google Patents

Resorptionsverfahren für Wärmepumpen Download PDF

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Publication number
EP0093051B1
EP0093051B1 EP83400795A EP83400795A EP0093051B1 EP 0093051 B1 EP0093051 B1 EP 0093051B1 EP 83400795 A EP83400795 A EP 83400795A EP 83400795 A EP83400795 A EP 83400795A EP 0093051 B1 EP0093051 B1 EP 0093051B1
Authority
EP
European Patent Office
Prior art keywords
heat
absorber
desorber
solution
gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
EP83400795A
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English (en)
French (fr)
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EP0093051A2 (de
EP0093051A3 (en
Inventor
Henri Rodié-Talbère
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Individual
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Individual
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Filing date
Publication date
Application filed by Individual filed Critical Individual
Priority to AT83400795T priority Critical patent/ATE46570T1/de
Publication of EP0093051A2 publication Critical patent/EP0093051A2/de
Publication of EP0093051A3 publication Critical patent/EP0093051A3/fr
Application granted granted Critical
Publication of EP0093051B1 publication Critical patent/EP0093051B1/de
Expired legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B25/00—Machines, plants or systems, using a combination of modes of operation covered by two or more of the groups F25B1/00 - F25B23/00
    • F25B25/02—Compression-sorption machines, plants, or systems
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
    • F25B15/12—Sorption machines, plants or systems, operating continuously, e.g. absorption type with resorber
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A30/00—Adapting or protecting infrastructure or their operation
    • Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/62—Absorption based systems

Definitions

  • the present invention relates to an improved process for heat pumps operating between two distinct temperature intervals according to the preamble of claim 1.
  • one of these temperature intervals is between a temperature level T1 and T2, on which the pump borrows from the heat to a cold source and the other between T3 and T4, on which it transfers heat to a hot source, these two temperature intervals not overlapping, the temperatures of the interval of the hot source being obviously higher to those of the cold source.
  • the process uses a gas called solute which undergoes in a liquid solvent at least one step of partial or total absorption during which heat is evacuated towards the hot source over the temperature interval T3-T4, this step being followed by at least one desorption step which takes place at a pressure lower than that of the absorption step and during which heat is received over the interval T1-T2.
  • the gas coming from a desorber is compressed to the pressure of the absorber and the temperature then reached in said absorber exceeds that of the gas during its compression. Compression is carried out for example by means of a compressor.
  • the heat exchanges therefore take place directly from the solution being enriched in the absorber, to the solution being depleted in the desorber, these two fluids being separated by a conductive wall.
  • exchanges are, for example, carried out by means of a heat transfer fluid contained in an enclosure constituting an exchange surface placed partly in the absorber and partly in the desorber, said fluid circulating in a closed circuit from the one to the other.
  • the heat transfer fluid can also be used to ensure exchanges with the hot source and / or with the cold source.
  • Heat exchanges between the system and hot and cold sources can be carried out using heat tubes, so as to eliminate any risk of contamination between the system and external sources.
  • the object of the present invention essentially consists in obtaining, on the one hand, a cycle having an amplitude of variation of the concentration of the solvent as wide as possible and, on the other hand, a temperature of the solvent preferably entering the resorber greater than that of the solvent leaving after enrichment; these two conditions having the essential consequence of allowing a significant reduction in the pressure difference.
  • the solution contained in the absorber is cooled below the temperature level which it would be possible to reach only by exchange with the external hot source, that is to say: T 3 , to the pinch; in this way its concentration of solute may be markedly high.
  • the desorption will be pushed beyond the concentration corresponding to the maximum temperature that allows the exchange with the cold source (T 2 , to the nearest pinch).
  • the heat required for desorption will be provided by the cooling of the resorber, which will thus increase the range of concentration variation.
  • the process according to the invention therefore makes it possible, on condition of performing the countercurrent exchanges between the fluids, to lower the temperature of the solution being enriched in the resorber below T 3 and, at the limit, to reach T 2 ; simultaneously the temperature of the depleted solution in the desorber will be raised above T 2 and may reach T 3 . Since the concentration variation range corresponding to the temperature interval T 1 -T 2 no longer has to correspond to that of the interval T 3 -T 4 , there will be a shift towards higher concentrations for the exchanges with the cold source, towards low concentrations for exchanges with the hot source, the additional concentration variation, with or without overlapping, corresponding to internal exchanges in the system.
  • the heat exchanges between the solution enriched in the absorber and that which is depleted in the desorber can optionally, and without departing from the scope of the present invention, be carried out directly through an exchanger wall or, indirectly, by means of a heat transfer fluid contained inside an enclosure whose walls constitute the exchange surface and one part of which is located in the desorber, the other in the resorber.
  • This heat transfer fluid will therefore heat up by cooling the solution in the absorber and then cool down by heating the solution in the desorber. It is also possible to circulate this fluid in the exchangers constituting the hot source and the cold source; it is this arrangement which has been illustrated by way of example of embodiment in the attached figure.
  • the exchanger E 1 being the desorber and the exchanger E 2 the resorber, the lean solution enters this last device by the conduit (1) and leaves it enriched by the conduit (2), after having been in contact with the gas introduced through the conduit (3).
  • the enriched solution is expanded in valve V, before being introduced into E, by (4) where it is desorbed before leaving it by (5). From there it is pumped by P l to the pressure of the absorber where it is again introduced.
  • the gas desorbed at E 1 is sent via line (6) to a compressor Ci from where, its pressure having been raised to the level of E 2, it is again introduced into this device.
  • the resorption cycle When the resorption cycle is associated with an absorption cycle, it is conventionally possible to operate the resorption cycle at a lower concentration, that is to say that the heat given off at the absorber will be at a temperature higher than that of the two desorbers.
  • the absorber and the absorber can be operated in a range between that of the high pressure desorber and that of the low pressure desorber.
  • the diagram then corresponds to the operation of a heat pump where the condenser and the evaporator are replaced by the absorber and the desorber. We then find the advantages already mentioned of exchanges over wide temperature intervals.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Sorption Type Refrigeration Machines (AREA)
  • Central Heating Systems (AREA)
  • Compressor (AREA)
  • Confectionery (AREA)
  • Compression-Type Refrigeration Machines With Reversible Cycles (AREA)

Claims (7)

1. Verfahren, bestimmt für Wärmepumpen, die zwischen zwei unterschiedlichen Temperaturintervallen arbeiten, das eine zwischen einem Temperaturniveau von T, und T2, in dem die Pumpe Wärme einer kalten Quelle entzieht und das andere zwischen T3 und T4, in dem sie Wärme an eine warme Quelle abgibt, wobei diese beiden Temperaturintervalle sich nicht überdecken, die Intervalltemperaturen der heißen Quelle offensichtlich höher als die der kalten Quelle liegen und beim Verfahren ein sogenanntes gelöstes Gas verwendet wird, das in einem flüssigen Lösungsmittel wenigstens eine Stufe der teilweisen oder totalen Absorption erfährt, während der Wärme gegen die heiße Quelle im Temperaturintervall T3-T4 abgeführt wird, wobei sich an diese Stufe wenigstens eine Stufe der Desorption anschließt, die bei einem Druck kleiner als dem der Absorptionsstufe abläuft und während der Wärme im Intervall Tl-T2 aufgenommen wird, dadurch gekennzeichnet, daß :
im Temperaturbereich zwischen den beiden genannten Intervallen Wärme zwischen dem Absorber und dem Desorber ausgetauscht wird, um die Amplitude der Konzentrationsveränderung des Lösungsmittels in Gelöstem zu strecken ;
das Gas in das heißeste Ende des Absorbers eingeführt und mit der verarmten Lösung kontaktiert wird und hierin wenigstens teilweise adiabatisch absorbiert wird, wobei die Lösung Wärme an die warme Quelle abgibt ;
die reiche Lösung am kalten Ende des Desorbers eingeführt wird, wo eine wenigstens teilweise Verdampfung durch Entspannen erreicht wird, wobei die gasförmige kalte Phase dann mit dem Gas vermischt wird, welche schließlich im heißesten Teil desorbiert wird, wobei das Ganze nach seiner Extraktion auf hohen Druck gebracht wird, während die verarmte Lösung den Desorber über ihr heißes Ende verläßt und auf den Druck des Absorbers gebracht wird, bevor sie in letzteren eingeführt wird.
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das aus einem Desorber kommende Gas bis auf den Druck des Absorbers komprimiert wird und daß die dann in diesem Absorber erreichte Temperatur die des Gases während seiner Kompression überschreitet.
3. Verfahren nach Anspruch 2, dadurch gekennzeichnet, daß die Kompression vermittels eines Kompressors (C1) vorgenommen wird.
4. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Wärmeaustauschervorgänge direkt von der im Anreicherungszustand in dem Absorber befindlichen Lösung gegen die im Verarmungszustand im Desorber befindliche Lösung vorgenommen werden, wobei diese beiden Fluide durch eine leitende Wand getrennt werden.
5. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Wärmeaustauschervorgänge vermittels eines Wärmeträgerfluids vorgenommen werden, der in einem umschlossenen Raum enthalten ist, der eine Wärmeaustauscherfläche bildet, die zum Teil im Absorber und zum Teil im Desorber angeordnet ist, wobei dieses Fluid in geschlossenem Kreislauf vom einen zum anderen zirkuliert.
6. Verfahren nach Anspruch 5, dadurch gekennzeichnet, daß das Wärmeträgerfluid auch dazu dient, die Austauschervorgänge mit der heißen Quelle und/oder der kalten Quelle sicherzustellen.
7. Verfahren nach Anspruch 4 oder Anspruch 5, dadurch gekennzeichnet, daß die Wärmeaustauschervorgänge zwischen dem System und den heißen und kalten Quellen mit Hilfe von Wärmerohren derart stattfinden, daß jede Gefahr einer Verschmutzung zwischen dem System und den äusseren Quellen beseitigt wird.
EP83400795A 1982-04-28 1983-04-21 Resorptionsverfahren für Wärmepumpen Expired EP0093051B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT83400795T ATE46570T1 (de) 1982-04-28 1983-04-21 Resorptionsverfahren fuer waermepumpen.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8207323A FR2526136B1 (fr) 1982-04-28 1982-04-28 Procede a cycle de resorption pour les pompes a chaleur
FR8207323 1982-04-28

Publications (3)

Publication Number Publication Date
EP0093051A2 EP0093051A2 (de) 1983-11-02
EP0093051A3 EP0093051A3 (en) 1984-09-19
EP0093051B1 true EP0093051B1 (de) 1989-09-20

Family

ID=9273492

Family Applications (1)

Application Number Title Priority Date Filing Date
EP83400795A Expired EP0093051B1 (de) 1982-04-28 1983-04-21 Resorptionsverfahren für Wärmepumpen

Country Status (4)

Country Link
EP (1) EP0093051B1 (de)
AT (1) ATE46570T1 (de)
DE (1) DE3380599D1 (de)
FR (1) FR2526136B1 (de)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4724679A (en) * 1986-07-02 1988-02-16 Reinhard Radermacher Advanced vapor compression heat pump cycle utilizing non-azeotropic working fluid mixtures
DE3716642A1 (de) * 1987-05-18 1988-12-08 Thermo Consulting Heidelberg Zweistoff-kompressions-waermepumpe bzw. expansionsmaschinen-anlage mit loesungskreislauf

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE142330C (de) *
DE278076C (de) * 1911-08-11
DE530406C (de) * 1928-12-23 1933-11-01 Siemens Schuckertwerke Akt Ges Verfahren zur Kaelteerzeugung
DE678942C (de) * 1932-12-22 1939-07-29 Siemens Schuckertwerke Akt Ges Einrichtung zur Waermeumwandlung
US2182453A (en) * 1936-01-18 1939-12-05 William H Sellew Heat transfer process and apparatus
DE867122C (de) * 1950-08-29 1953-02-16 Edmund Dr-Ing E H Altenkirch Verfahren und Vorrichtung zum Heben der einem Waermetraeger entzogenen Waermemenge niedrigerer Temperatur auf eine hoehere Temperatur
SE419479B (sv) * 1975-04-28 1981-08-03 Sten Olof Zeilon Kylalstringsforfarande och apparatur for utovning av forfarandet
DE2807990A1 (de) * 1978-02-23 1979-08-30 Vaillant Joh Gmbh & Co Sorptionswaermepumpe
DE2838780A1 (de) * 1978-09-06 1980-03-20 Vaillant Joh Gmbh & Co Resorptionswaermepumpe
DE2910288A1 (de) * 1979-03-15 1980-09-25 Vaillant Joh Gmbh & Co Waermepumpe, insbesondere strahl- kompressions-waermepumpe
FR2454591A1 (fr) * 1979-04-17 1980-11-14 Inst Francais Du Petrole Procede perfectionne de production de froid et/ou de chaleur au moyen d'un cycle a absorption
HU186726B (en) * 1979-06-08 1985-09-30 Energiagazdalkodasi Intezet Hybrid heat pump
DE3100348A1 (de) * 1981-01-08 1982-08-05 Dieter Dr.-Ing. 5064 Rösrath Markfort "resorptions-anlage zur waermetransformtation"

Also Published As

Publication number Publication date
FR2526136B1 (fr) 1986-05-30
ATE46570T1 (de) 1989-10-15
EP0093051A2 (de) 1983-11-02
DE3380599D1 (en) 1989-10-26
EP0093051A3 (en) 1984-09-19
FR2526136A1 (fr) 1983-11-04

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